Pulse detonation shockwave gasifier

ABSTRACT

Gasifiers, gasification systems, and methods for producing synthesis gas are disclosed. A gasifier can include a gasifier body. A feeder can be positioned to feed an organic material into the gasifier body. A pulse detonation burner can be located under or above the gasifier body and connected to the gasifier body to direct supersonic shockwaves upward into the gasifier body to heat the organic material and to form a jet spouted bed of the organic material or to operate as an entrained flow reactor. An outlet can be located at the gasifier body to allow removal of synthesis gas, residual ash, and other reaction products.

RELATED APPLICATION

This application is a continuation-in-part of U.S. application Ser. No.16/005,432, filed Jun. 11, 2018, entitled “Pulse Detonation ShockwaveGasifier” which is incorporated herein by reference.

FIELD OF THE INVENTION

The present technology relates generally to methods and apparatus forproducing reducing gases, commonly known as synthesis gas or syngas, bygasifying carbonaceous material.

BACKGROUND

Gasification systems may be used to form fuel-gas, syngas, a mixture ofgases including carbon monoxide and hydrogen. Syngas is often used as afuel or as a feedstock for forming other compounds. Gasificationtypically involves heating a carbonaceous material, such as biomass, toconvert hydrocarbons in the material into carbon monoxide and hydrogengases. Besides syngas, other products from a gasification reactor mayinclude methane, acetylene, ethylene, and other low-molecular weightgases, volatile organic vapors, aerosol-tars, carbon-char, and residualcarbonaceous mineral ashes. The energy requirements of gasificationreactors can be substantial, while the aerosol-tars and carbon-char canpose problems for the energy conversion equipment, while lowering netconversion efficiency. Reforming of the tars and carbon-char may beperformed, but this can add significantly to costs and energyrequirements associated with the process.

SUMMARY

In some examples of the present technology, a gasifier can include agasifier body, a feeder, a pulse detonation burner, and an outlet. Thefeeder can be positioned to feed an organic material into the gasifierbody. The pulse detonation burner can be located under the gasifier bodyand connected to the gasifier body such that the pulse detonator directssupersonic shockwaves upward into the gasifier body. The inverseposition is also possible, so that the pulse detonation burner can alsobe located on top of the gasifier body and connected to the gasifierbody such that the pulse detonator directs supersonic shockwavesdownward into the gasifier body acting as an entrained flow reactor. Thesupersonic shockwaves can both heat the organic material and form a jetspouted bed of the organic material in the gasifier body. The outlet canbe located at an upper portion of the gasifier.

In further examples, a gasification system can include a gasifier asdescribed above and a reformer connected to the outlet of the gasifier.The reformer can receive synthesis gas and residual material from thegasifier. The reformer can include a reformer body and a second pulsedetonation burner located above the reformer body. The second pulsedetonation burner can be connected to the reformer body to directsupersonic shockwaves downward into the reformer body to heat thesynthesis gas and residual material. The inverse position is alsopossible, so that the reformer can include a reformer body and a secondpulse detonation burner located below the reformer body. The secondpulse detonation burner can be connected to the reformer body to directsupersonic shockwaves upward into the reformer body to heat thesynthesis gas and residual material.

In other examples of the present technology, a method of producingsynthesis gas can include introducing an organic material into agasifier. The gasifier can include a gasifier body and a pulsedetonation burner located under the gasifier body. Supersonic shockwavescan be fired from the pulse detonation burner upward into the gasifierbody to heat the organic material and form a jet spouted bed of theorganic material. Synthesis gas and residual ash can be removed from thegasifier through an outlet located at an upper portion of the gasifierbody.

There has thus been outlined, rather broadly, the more importantfeatures of the invention so that the detailed description thereof thatfollows may be better understood, and so that the present contributionto the art may be better appreciated. Other features of the presentinvention will become clearer from the following detailed description ofthe invention, taken with the accompanying drawings and claims, or maybe learned by the practice of the invention.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic view of an example gasifier in accordance with anexample of the present technology.

FIG. 2 is a schematic view of an example gasification system inaccordance with an example of the present technology.

FIG. 3 is a block flow diagram of another example gasification system inaccordance with an example of the present technology.

FIG. 4 is a schematic view of yet another example gasification system inaccordance with an example of the present technology.

FIG. 5 is a flowchart of an example method of producing synthesis gas inaccordance with an example of the present technology.

These drawings are provided to illustrate various aspects of theinvention and are not intended to be limiting of the scope in terms ofdimensions, materials, configurations, arrangements or proportionsunless otherwise limited by the claims.

DETAILED DESCRIPTION

While these exemplary embodiments are described in sufficient detail toenable those skilled in the art to practice the invention, it should beunderstood that other embodiments may be realized and that variouschanges to the invention may be made without departing from the spiritand scope of the present invention. Thus, the following more detaileddescription of the embodiments of the present invention is not intendedto limit the scope of the invention, as claimed, but is presented forpurposes of illustration only and not limitation to describe thefeatures and characteristics of the present invention, to set forth thebest mode of operation of the invention, and to sufficiently enable oneskilled in the art to practice the invention. Accordingly, the scope ofthe present invention is to be defined solely by the appended claims.

Definitions

In describing and claiming the present invention, the followingterminology will be used.

It is noted that, as used in this specification and in the appendedclaims, the singular forms “a,” “an,” and “the” include plural referentsunless the context clearly dictates otherwise. Thus, for example,reference to “an outlet” includes one or more of such features,reference to “a material” includes reference to one or more of suchelements, and reference to “removing” includes reference to one or moreof such steps.

As used herein, the term “about” is used to provide flexibility andimprecision associated with a given term, metric or value. The degree offlexibility for a particular variable can be readily determined by oneskilled in the art. However, unless otherwise enunciated, the term“about” generally connotes flexibility of less than 5%, and most oftenless than 1%, and in some cases less than 0.01%.

As used herein, the term “substantially” refers to the complete ornearly complete extent or degree of an action, characteristic, property,state, structure, item, or result. The exact allowable degree ofdeviation from absolute completeness may in some cases depend on thespecific context. However, the nearness of completion will generally beso as to have the same overall result as if absolute and totalcompletion were obtained. “Substantially” refers to a degree ofdeviation that is sufficiently small so as to not measurably detractfrom the identified property or circumstance. The exact degree ofdeviation allowable may in some cases depend on the specific context.The use of “substantially” is equally applicable when used in a negativeconnotation to refer to the complete or near complete lack of an action,characteristic, property, state, structure, item, or result.

As used herein, a plurality of items, structural elements, compositionalelements, and/or materials may be presented in a common list forconvenience. However, these lists should be construed as though eachmember of the list is individually identified as a separate and uniquemember. Thus, no individual member of such list should be construed as ade facto equivalent of any other member of the same list solely based ontheir presentation in a common group without indications to thecontrary.

As used herein, the term “at least one of” is intended to be synonymouswith “one or more of.” For example, “at least one of A, B and C”explicitly includes only A, only B, only C, and combinations of each.

Concentrations, amounts, and other numerical data may be presentedherein in a range format. It is to be understood that such range formatis used merely for convenience and brevity and should be interpretedflexibly to include not only the numerical values explicitly recited asthe limits of the range, but also to include all the individualnumerical values or sub-ranges encompassed within that range as if eachnumerical value and sub-range is explicitly recited. For example, anumerical range of about 1 to about 4.5 should be interpreted to includenot only the explicitly recited limits of 1 to about 4.5, but also toinclude individual numerals such as 2, 3, 4, and sub-ranges such as 1 to3, 2 to 4, etc. The same principle applies to ranges reciting only onenumerical value, such as “less than about 4.5,” which should beinterpreted to include all of the above-recited values and ranges.Further, such an interpretation should apply regardless of the breadthof the range or the characteristic being described.

Any steps recited in any method or process claims may be executed in anyorder and are not limited to the order presented in the claims.Means-plus-function or step-plus-function limitations will only beemployed where for a specific claim limitation all of the followingconditions are present in that limitation: a) “means for” or “step for”is expressly recited; and b) a corresponding function is expresslyrecited. The structure, material or acts that support the means-plusfunction are expressly recited in the description herein. Accordingly,the scope of the invention should be determined solely by the appendedclaims and their legal equivalents, rather than by the descriptions andexamples given herein.

Reference will now be made to the exemplary embodiments illustrated, andspecific language will be used herein to describe the same. It willnevertheless be understood that no limitation of the scope of thetechnology is thereby intended. Additional features and advantages ofthe technology will be apparent from the detailed description whichfollows, taken in conjunction with the accompanying drawings, whichtogether illustrate, by way of example, features of the technology.

With the general examples set forth in the Summary above, it is noted inthe present disclosure that when describing the system, or the relateddevices or methods, individual or separate descriptions are consideredapplicable to one other, whether or not explicitly discussed in thecontext of a particular example or embodiment. For example, indiscussing a device per se, other device, system, and/or methodembodiments are also included in such discussions, and vice versa.

Furthermore, various modifications and combinations can be derived fromthe present disclosure and illustrations, and as such, the followingfigures should not be considered limiting.

Pulse Detonation Shockwave Gasifiers

The present technology involves gasifiers that utilize supersonicshockwaves created by pulse detonation burners to gasify organicmaterial. These gasifiers can be incorporated into gasification systemsthat may also include a pulse detonation burner-powered reformer.

In some examples, the technology described herein can be used as amodification of the systems and processes disclosed in U.S. Pat. No.5,584,255, which is incorporated herein by reference. In certainexamples, the gasifier can volatize organic feed materials by employinga mixture of fuel and oxygen, which burns to form high-temperaturecarbon dioxide and water vapor that are injected into the gasifier. Theextreme heat and the presence or absence of free oxygen can cause theorganic feed materials to volatilize and dissociate into a mixture ofsyngas, volatile organic compounds, carbon-char, and residual mineralash. The gasifier can be used as the first stage in a gasificationprocess. Inputs into the gasifier can include both heat and mechanicalenergy from a pulse-detonation burner. A second stage of thegasification process can include a reformer integrated in the process insuch a way that the reformer lowers the energy requirements for syngasproduction. The reformer can function to convert the volatile organiccompounds, including tar vapors and carbon-char from the gasificationreactor, into fuel-gas and synthesis gases, employing heat input as hotgases that include oxidizing and reducing gases, and mechanical energysupplied by shockwaves discharged from a pulse-detonation burner.

In further examples, the gasifier can employ a robust jet-spouted bedfor the primary gasification stage. The exhaust itself ejected from thepulse detonation burner can be used to form the jet of the jet-spoutedbed. By incorporating pulse-detonation technology, several benefits canbe achieved because the jet-spouted bed can utilize shockwave momentumas a source of power input. A jet spouted bed is formed by a bottominlet for gases that discharges into a conical expanded bed, wherein alow-density bed composed of organic or inorganic materials iscirculated, bed materials are comminuted, and elutriated by the inletgas and product gases. In some examples, pulse detonation burners candischarge shockwaves with supersonic velocities up to about 3,000 metersper second. The supersonic compression waves can compress moleculesclose together, increasing the rate of thermal chemical reactivity atthe molecular level. Additionally, the compression waves can enhancecomminution of the organic feed material at the macro-level. Rapidmixing and comminution of the feed can also enable the use of relativelycoarse feed materials.

The gasifiers, systems and processes described herein can usepressure-gain-combustion methods to increase process-intensity. Aproblem with traditional gasification methods is that increasing processintensity can also increase parasitic power consumption. For example,employing high-temperature plasma burners to enable tar cracking andcarbon-char reforming can increase process intensity, but can alsoincrease the cost of parasitic power consumption. In contrast, the useof pulse-detonation burners can increase process intensity andconcurrently reduce parasitic power consumption. Moreover, the pulsecombustion hardware can be fabricated and operated at low cost comparedto many other intensification methods. In some examples, a pulsedetonation burner can be constructed using a tubular combustion chamber,with or without cooling means, with fuel and air or oxygen inputs,combined with a cyclic ignition system.

In certain examples of the present technology, a pulse-detonation burnercan produce heat in the form of hot-exhaust gases and mechanical powerto drive materials circulation within a jet-spouted bed gasifier. Thegasifier can serve as the devolatilization stage in a gasificationprocess. In a second stage of the process, a reformer can also bepowered by the heat and mechanical power produced by a secondpulse-detonation burner. The reformer can also operate similarly to aventuri ejector. The gases produced by the second pulse detonationburner can act as a motive fluid to draw the effluent from the gasifierinto the reformer. Tars and carbon-char in the effluent of the gasifiercan be converted into more syngas using the reformer. This can providean energy efficient process to mitigate environmental risks posed by thebyproducts of the gasifier.

In both the gasifier and the reformer, the supersonic compression wavesgenerated by the pulse detonation burners can enhance the reaction rateof molecules by pushing the molecules closer together each time acompression wave passes through. Although the gasifier and reformer maybe operated at or near atmospheric pressure, the compression waves fromthe pulse detonation burners can mimic operating the gasifier andreformer at an elevated pressure. The compression waves can also enhancemixing of the materials in the gasifier and reformer, as well ascomminute solid organic and mineral materials to smaller particle sizes.All these effects can increase reaction rates in the gasifier andreformer.

In further examples, the gasification process can be operated at atemperature below the ash-fusion temperature. For example, the gasifierand reformer can be operated at a temperature of 1150° C. or less. Somehigh-temperature gasifiers operate above the ash-fusion temperature,such as at temperatures of 1300° C. to 1450° C. At these temperaturesmolten mineral ashes flow at low viscosity, and this can incur a highoxygen cost and refractory problems. To avoid these problems, thegasifiers and/or reformers described herein can operate, in someexamples, at a temperature from 920° C. to 1150° C. In further examples,the gasifier and reformer can operate at a temperature from 1050° C. to1250° C.

With this description in mind, FIG. 1 shows a schematic of a gasifier100 in accordance with an example of the present technology. Thegasifier includes a gasifier body 110, a feeder 120, and a pulsedetonation burner 130. In this example, the gasifier body includes aconical portion 112 expanding upward from the bottom of the gasifierbody. The pulse detonation burner can be supplied with air, oxygen, oroxygen enriched air through air line 132 and fuel through fuel line 134.The feeder can be positioned to feed an organic material that mayinclude mineral matter into the gasifier body. The pulse detonationburner is located under the gasifier body and connected to the gasifierbody to direct supersonic shockwaves upward into the gasifier body. Theshockwaves and hot gas produced by the pulse detonation burner can heatthe organic material and form a jet spouted bed of the organic materialin the gasifier body. Syngas can be produced in the gasifier. The syngasand any residual materials, such as organic vapors, tar, carbon-char,and mineral ashes, can flow out of the gasifier through an outlet 140.

In this example, the feeder feeds organic material into an inlet locatedon a side of the gasifier body part-way up the height of the gasifierbody. In some examples, the feeder can be positioned to feed the organicmaterial into an entrainment zone within the gasifier body, enabling thegasifier to be fired in the downward direction, thereby operating thegasifier body as an entrained flow reactor. The feeder can move organicmaterial into the gasifier body in a variety of ways. In some examples,the feeder can include an extrusion feeder, auger, hydraulic ram,conveyor belt, gravity-fed hopper, or combinations thereof.

The organic material fed into the gasifier can include industrialorganic waste, agricultural waste, domestic organic waste, municipalsolid waste, coal, biomass, post-sorted refuse derived biomass, orcombinations thereof that may include a significant fraction of mineralmatter. In certain examples, the organic material can be a type of wetor dry organic waste, including sewage and sewage-sludge, human andanimal wastes, and various types of wet and dry manure.

As a general guideline, the organic feed material can be a dry fibrousor particulate material, with less than 1% moisture, although in somecases can contain up to 99% water. In further examples, the organicmaterial can have an average particle size from 1 mm to 10 cm. In mostcases, the organic material can have an average particle size from 5 mmto 3 cm. In certain examples, the organic material can have a relativelylarger coarse particle size than would otherwise be used in a spoutedbed gasifier because the supersonic shockwaves produced by the pulsedetonation burner can crush the particles to smaller sizes within thegasifier. In further examples, the organic material can initially havean average coarse particle size of 2 cm to 10 cm. As used herein,“particle size” refers to the diameter of a spherical particle or thelongest dimension of a non-spherical particle. Additionally, “averageparticle size” refers to the number average particle size of theparticles in the organic material fed into the gasifier. The feedmaterials are typically pre-shredded or otherwise size-reduced; forexample, using a rotary-shear machine that is commonly used tosize-reduce paper, plastic, fibers, wood, municipal solid wastes, andother organic materials that include inherent mineral matter up to about45%. The feed materials that result from size-reduction typically havenon-uniform dimensions and include fine particulate matter, fibrousmaterials, as well as sheets and flakes.

The pulse detonation burner used to supply energy to the gasifier caninclude a detonation chamber or zone connected to the gasifier body suchthat when fuel is detonated in the chamber, reaction products of thedetonation are directed into the gasifier body. A discharge zone canalso be oriented adjacent the detonation zone in order to allowcombustion products to be exhausted from the burner body near themaximum theoretical velocity by employing internal shapes that form anozzle, which can be of the converging/diverging type, with a convergingnozzle angle between 7-degrees and 67-degrees and a diverging anglebetween 0-degrees and 90-degrees. The discharge zone, i.e. the expansionzone, can be constructed of metal, ceramic, or formed form refractorycement. The discharge zone, i.e. the expansion zone, typically includesmeans to inject gases, liquids, and solids, singularly or incombinations, including ternary mixtures of carbon-char particles andliquid-tars that are entrained by low-pressure steam, injected into thedischarge zone through openings that can be annular, recessed tominimize turbulence, and directed in the direction for the expandingshockwaves. The pulse detonation burner can be located beneath thegasifier and oriented upward so that the reaction products form anupward moving gas jet to fluidize organic material in the gasifier body.Alternatively, the pulse detonation can be directed downward into thegasification body so that the gasifier acts as an entrained flowreactor. In certain examples, the detonation chamber can be a hollowtube. The tube can generally have a diameter from 1 cm to 50 cm, forexample, and can be air-cooled or water-cooled. In further examples, thetube can have a length from 12 cm to 600 cm, and often from 80 cm to 160cm. In various examples, the detonation chamber can be formed of anymaterial that can withstand the high pressures and temperatures producedby the detonations. Some non-limiting examples of materials used in thedetonation chamber can include steel, stainless steel, copper, nickel,tungsten, tantalum, molybdenum, niobium, aluminum, and alloys thereof Inother examples, the detonation chamber can include a ceramic material.Copper construction is particularly useful because of its superiorheat-transfer capability, which enables air cooling or water cooling ofthe pulse detonation chamber in order to maintain discrete detonationevents, as compared to the formation of continuous or semi-continuousdeflagrations.

The pulse detonation burner can also include a fuel inlet connected to afuel source. In some examples, the fuel detonated in the pulsedetonation burner can include a hydrocarbon such as natural gas, ethane,propane, butane, gasoline, and so on. In other examples, the fuel caninclude syngas. In some cases, a portion of fuel-gas or syngas producedby the gasification process can be used to fuel the pulse detonationburner. For example, product gases containing hydrogen and unsaturatedhydrocarbons, exemplified by light olefins, particularly includingacetylene, ethylene, and propylene, are particularly attractive becauseof the ability to form explosive mixtures with air or oxygen enrichedair. In still further examples, the fuel can include residual carbonchar that is left as a byproduct of the gasification process that isthereby recycled into the gasification process, and may include mineralmatter that serves as a catalyst to either the detonation process or thegasification process. Additional suitable fuels can includemicronized-carbon sourced from biochar, torrefied biomass, and coalfines. Micronized solids can be conveyed into the detonation zone of thedetonation burner by one or more carrier fluids, such as fuel-gases orliquid-fuels that serve as the carrier fluid. Non-limiting examples ofsuch carrier fluids include hydrogen, methane, syngas, producer-gas,steam, kerosene, methanol, and combinations of these or similar fluids.

An oxygen inlet can supply oxygen to the detonation chamber to detonatewith the fuel. In some examples, the oxygen inlet can simply supplyplain air to the detonation chamber. In other examples, the oxygen inletcan supply pure oxygen or oxygen-enriched air. In some cases,oxygen-enriched air can include from about 30 mol % to 90 mol % oxygen,and in some cases up to 99.9 mol %. Gaseous air enriched from about 33mol % oxygen to about 70 mol % oxygen is particularly advantageousbecause the production cost is modest compared to production cost of airenriched to greater than 90 mol % oxygen and the pulse detonationprocess can tolerate the presence of fuel diluents, including nitrogen,carbon dioxide, and water vapor.

In certain examples, the ratio of fuel to air employed by the pulsedetonation burner can be either fuel-rich or fuel-lean, depending on theneed for reducing gases or oxidizing gases within the gasification andreforming processes. The power output generated by the pulse detonationburner is not strictly tied to the combustion stoichiometry, andtherefore both fuel-rich and fuel-lean stoichiometry can be successfullyemployed. The range for the ration of fuel to air is typically from 1:1to 1:50 by weight. In further examples, the ratio can be from 1:5 to1:25 or from 1:10 to 1:20. The optimal fuel to air ratio may varydepending on the type of fuel used and the amount of oxygen in the air,for example. Availability of free oxygen is desirable when autothermalgasification and partial oxidation are process objectives within thegasifier and the reformer. In some examples, the exhaust gas from thepulse detonation burner can contain more than 20% free oxygen and atleast 12% carbon oxides and at least 3% water vapor. In furtherexamples, the exhaust gas can contain from 5% to 10% free oxygen, 12% to30% carbon oxides, and from 3% to 10% water vapor. In some examples, thedetonation exhaust gases will contain up to 40% hydrogen and less than2% free oxygen, in the case when reducing gases are needed with thegasification or reforming zones. In an example, the pulse detonationchamber is operated with fuel and air input at about the stoichiometricratio, with neither excess fuel or excess air, and then diluent air ismixed with the detonation exhaust gases to generate a mixed stream ofhot oxidizing gases that are used for autothermal gasification. In onenon-limiting example, the oxygen flows continuously into the detonationburner mixing chamber, the detonations occur during fuel-richconditions, operating with a target of Phi=1.33 for the oxygen-fuelmixture achieved during the detonation phase; oxygen continues to flowduring a short purge phase following each detonation, thereby causingthe detonation burner-exhaust to contain excess oxygen for the instantbetween fuel-injections, thus providing an excess of O₂, along with H₂Oand CO₂, in the burner exhaust, all of which exist as superheatedexhaust-products that participate in partial-oxidation reactionsassociated with shockwave enhanced gasification of organic feeds. Instill another optional aspect, CO₂ can be recycled into the detonationzone of the detonation burner, or injected into the discharge zone. TheCO₂ can be obtained from the gasifier outlet, reformer, or other unitsas described herein, or obtained from external sources of CO₂ that areintended for recycle into the detonation burner discharge zone, alsoknown as the expansion zone, where thermochemical reactions areintensified to the extent that CO₂ serves as an oxidant that reacts withcarbon, enabling the partial-oxidation of carbon, thereby forming largequantities of gaseous carbon monoxide, CO, a valuable constituent ofsynthesis gas used to produce synthetic jet fuel, for example. In oneexample, carbon dioxide, gases bearing CO_(2,) can serve as carriergases for entrained particulate solids, including carbon-char, or anytransition-metal or mineral catalyst selected from a list of activematerials that include calcium oxide, calcium carbonate, and potassiumcarbonate. Liquids, including aqueous emulsions with tar-liquids, canlikewise be injected along with CO₂ into the detonation zone of thedetonation burner, or injected into the discharge zone, also known asthe expansion zone.

As another optional example, the pulse detonation burner can includesupplemental reactants in addition to the fuel and air/oxygen. Forexample, low-pressure steam can be injected into the pulse detonationburner. Such steam can also be injected downstream from the pulsedetonation burner or in a discharge section of a tube (i.e. body) of thepulse-detonation burner, where thermochemical reactions are intensifiedto the extent that H₂O serves as an oxidant that reacts with carbon,enabling the partial-oxidation of carbon, thereby forming largequantities of gaseous hydrogen, H₂, a valuable constituent of synthesisgas used for production of high-purity hydrogen gas, for example. Lowpressure steam can generally be steam below about 50 psig, while in thecontext of a high-pressure Rankine-cycle steam plant, low-pressure canbe up to 300 psig. In one example, low-pressure steam can serve ascarrier gases for entrained particulate solids, including carbon-char,bio-char, torrefied carbon, or any transition-metal or mineral catalystselected from a list of active materials that include calcium oxide,calcium carbonate, and the various form of potassium including potassiumcarbonate. Liquids, including aqueous emulsions with organic tars, canlikewise be injected using low-pressure steam as the driving force toentrained liquids or solids injected into the detonation zone of thedetonation burner, or injected into the discharge zone, also known asthe expansion zone.

In some examples, the detonation of fuel with air, oxygen, oroxygen-enriched air can create shockwaves that travel at speeds of 100meters per second to 3,000 meters per second, and in some cases greaterthan 150 meters per second. In further examples, the shockwaves cantravel at speeds from 500 meters per second to 2,000 meters per second.The pulse detonation burner can thus be different from pulsedeflagration burners, which discharge at lower speeds of around 10 to100 meters per second.

The pulse detonation burner can also include a cyclic ignition systemthat can ignite the fuel inside the detonation chamber at pulsedintervals. In some examples, the detonations can have a frequency of atleast 2 Hz. In further examples, the detonations can have a frequencyfrom 2 Hz to 100 Hz. In certain examples, the frequency of thedetonations can be selected and/or actively controlled to maintain aparticular operating temperature within the gasifier. For example, thegasifier operating temperature may be from 920° C. to 1150° C. or from1050° C. to 1550° C. In some examples, the temperature of the hot gasproduced by the pulse detonation burner can be from 750° C. to 1250° C.Furthermore, the pulse detonation burner can produce hot gas at atemperature from 750° C. to 1550° C., and in some cases up to 3000° C.or from about 2000° C. to 3000° C. The average exhaust gas temperatureis typically in the 750° C. to 1550° C. range. The near-instantaneoustemperature achieved at or near the peak pressure achieve during thedetonation cycle is significantly higher than the average exhausttemperature, and the peak temperature is more difficult to measure. Thehigher instantaneous temperature (e.g. 2000° C. to 3000° C.) of thedetonation burner applies the secondary detonation burner used toaccomplish reforming. The gasifier body itself can be designed tooperate as a jet spouted bed reactor. In some examples, the gasifierbody can include a conical portion tapering toward the pulse detonationburner at the bottom of the gasifier body. The conical portion can allowthe hot gas stream from the pulse detonation burner to expand and form ajet spouted bed. The jet spouted bed is formed within a conical expandedbed section, which enables vigorous recirculation of bed materialscausing comminution of the organic and inorganic solids retained withinthe low-density expanded bed that defines the jet spouting action knownto those skilled in the art of fluidization. The gasifier body may alsoinclude a cylindrical portion above the conical portion. In some cases,heavy particles of organic material can move upward in the jet of hotgas from the pulse detonation burner and then disengage from the movinggas in the cylindrical portion of the gasifier body, at which point theheavy particles may fall back down and become entrained again in the hotgas stream. The height of the gasifier body can be sufficient to allowsuch heavy particles of organic material to become disengaged fromupward flow so that the heavy particles do not flow out the outlet atthe top of the gasifier body. In certain examples, the gasifier body canbe from 2 meters to 30 meters tall. In further examples, the gasifierbody can have a diameter from 10 cm to 7 m in the cylindrical portion.

The present technology also extends to gasification systems that caninclude a gasifier as described above, and can include one or moreadditional process units. In some examples, a gasification system caninclude a gasifier and a reformer. FIG. 2 shows one example of such agasification system 200. The system includes a gasifier 202 and areformer 204. Similar to the gasifier shown in FIG. 1, the gasifierincludes a gasifier body 210, a feeder 220, and a pulse detonationburner 230. A conical portion 212 of the gasifier body expands upwardfrom the bottom of the gasifier body. The pulse detonation burner can besupplied with air or oxygen enriched air through air line 232 and fuelthrough fuel line 234. The feeder can be positioned to feed an organicmaterial into the gasifier body. Syngas and residual materials, such asorganic vapors, tar, carbon-char, and mineral ashes, can flow out of thegasifier through an outlet 240.

The reformer 204 can receive the syngas and residual materials from theoutlet 240 of the gasifier 202. In some examples, the reformer canconvert at least some of the residual materials into additional syngas.In this example, the reformer includes a reformer body 250 and a secondpulse detonation burner 260 located above the reformer body. The secondpulse detonation burner can be connected to the reformer body to directsupersonic shockwaves downward into the reformer body to heat thesynthesis gas and residual material. The second pulse detonation burnercan also include a second air line 262 and a second fuel line 264 toprovide air or oxygen enriched air and fuel to the second pulsedetonation burner. The reformer can operate similarly to a venturiejector. The reformer body can include a venturi constriction 270 todecrease pressure inside the reformer and draw the effluent from thegasifier into the reformer. Specifically, the pressure in the throat ofthe venturi constriction is reduced due to the increase in velocity ofthe fluid flowing through the constriction. The reduced pressure causesa suction force to draw effluent product gases from the outlet of thegasifier into the reformer, and creates a low pressure in the feed inputzone. The low pressure zone in the feeding region can range from 3inches-water-column-vacuum up to about 27 inches water-column-vacuum,that is, from about 0.1 psig below ambient pressure up to about 1-psigbelow ambient pressure.

In terminology used with venturi ejectors, the hot exhaust gasesinjected by the second pulse detonation burner are the “motive fluid” or“driving fluid” and the effluent from the gasifier is the “suctionfluid.” The heat and mechanical energy provided by the second pulsedetonation burner can convert unreacted residuals in the gasifiereffluent into additional syngas. The product gases from the reformer,including syngas and remaining residual materials, can flow out of thereformer through reformer outlet 280. In the example shown in FIG. 2,the reformer also has an ash outlet 290 where ash can be removed fromthe reformer.

In various examples, gasification systems can include other processunits in addition to the gasifier and reformer shown in FIG. 2. As anexample, in some cases the crude syngas flowing out of the outlet of thereformer can undergo additional processing such as syngas cleaning andwater-gas shift reaction. Furthermore, multiple stages may be used forany of the process units, such as multiple gasification stages ormultiple reforming stages. In particular, hot cyclone separators aretypically installed in sequence following gasification and reforming toremove a mixture of carbon-char and mineral ashes. Hot cycloneseparators can typically be installed down-stream from the gasifier ordown stream from the reformer, and multiple hot cyclones can be operatedin series or in parallel. Hot cyclone separators are usually an integralpart of the gasification and reforming process and their operation isenhanced by the means of high velocity gas flow generated by the pulsedetonation burners.

During startup of the gasification system, the pulse detonation burnerconnected to the gasifier may be used to supply heat to heat up thegasifier to operating temperature. When the gasifier reaches theoperating temperature, the pulse detonation burner may continue tosupply heat to maintain the operating temperature and oxygen toaccomplish the autothermal gasification process. Similarly, the secondpulse detonation burner connected to the reformer can be used duringstartup to supply heat to heat up the reformer and to supply oxygen foruse in partial-oxidation in the reforming process. When the reformerreaches the operating temperature, the second pulse detonation burnercan continue to supply heat to maintain the operating temperature. Insome examples, the gasifier and the reformer can each have an operatingtemperature from 720° C. to 1150° C. or from 850° C. to 1250° C. Thereforming stage is typically operated at a higher temperature comparedthe gasifier temperature, so that the temperature profile is increasingfrom the gasification stage to the reforming stage. The gasifier andreformer can each be started and stopped safely under controlledconditions by starting and stopping the pulse detonation burners.

The high temperature and presence or absence of free oxygen in thegasifier can cause organic feed materials in the gasifier to volatilizeand dissociate into a mixture of syngas, volatile organic compounds,tar-vapors, carbon-char, and residual mineral ashes. This mixture can bedirected to flow into the reformer. As explained above, the reformer canoperate similarly to a venturi ejector to draw the effluent from thegasifier into the reformer and help to drive the flow of the productsthrough the remainder of the process. The second pulse detonation burnercan inject hot exhaust gases composed of either oxidizing or reducinggases into the reformer to drive the venturi flow through the reformer.The hot exhaust gases can also provide sufficient heat to convertresidual materials in the gasifier effluent to additional syngas. Thesecond pulse detonation burner can produce hot exhaust gases at atemperature from 750° C. to 1550° C., and in some cases up to 3000° C.Cyclic detonations of ternary methane-oxygen-steam mixtures are provedto generate highly superheated steam with temperature exceeding 2000° C.when expanded to the atmospheric pressure. The detonation products ofstoichiometric ternary mixtures under consideration can contain up to80% highly superheated and up to 17% CO₂ with various amounts of CO, O₂,and H₂. As a result of deep thermal processing (gasification) of organicwastes by such exhaust products, a gaseous mixture of CO and H₂ isobtained, which can be used to produce synthetic fuels, includingrenewable methane, CH₄, also known as renewable natural gas (RNG). Thekinetics for the gasification reactions improve significantly as thetemperature of reactants is increased. The hot exhaust products,including H₂O, CO₂, CO, and H₂, serve as chemical reactants in theorganic gasification process. The maximum temperature that the reactantscan reach as a result of cyclic detonation is very high, and thehigh-temperature conditions persist for about 2-miliseconds, which islong enough to increase productivity. The frequency of detonations inthe second pulse detonation burner can be at least 2 Hz, for examplefrom 2 Hz to 100 Hz. The exhaust gases can contain at least 10% oxygen,and 12% carbon oxides and at least 3% water vapor. For example, theexhaust gases can contain from 5% to 40% oxygen, 12% to 30% carbonoxides and from 3% to 10% water vapor. Under reducing conditions, forexample, the exhaust gases can contain from 10% to 40% hydrogen. Thesecond pulse detonation burner can be operated with any of the otherparameters described above with respect to the first pulse detonationburner, such as fuel type, amount of oxygen in the air supplied to thepulse detonation burner, fuel to air ratio, and so on. In some examples,the pulse detonation burner powering the gasifier and the second pulsedetonation burner powering the reformer can be operated withsubstantially the same operating parameters. In other examples, thepulse detonation burners can be operated with different operatingparameters; both can be used to generate hot oxidizing gases, or bothsupplying hot reducing gases, or one can supply hot oxidizing gases theother suppling hot reducing gases. In one example embodiment, bothburners supply hot oxidizing gases that contain greater than 10% freeoxygen required to accomplish autothermal gasification within thegasifier and used for partial oxidation within the reforming section.

FIG. 3 is a block flow diagram of another example gasification system300. In this system, the process of forming syngas begins with loosefeed material, which is fed using a feeding system 310 into agasification stage 320. In some examples, the feeding system can includeequipment to comminute the feed material and/or transport the feedmaterial at a controlled rate into the gasifier. The gasification stagecan include one or more gasifiers as described above. Effluent from thegasification stage can flow into a reforming stage 330. The reformingstage can include one or more venturi-type reformers as described above.The reforming stage can produce crude fuel-gas or crude syngas, whichthen flows into a gas cleaning stage. The gas cleaning stage canseparate fine particulate solids from the fuel gases or from thesynthesis gases, and steam is typically removed by cooling the productgases during this stage and is recovered as water condensate. The steamand fuel gases can be utilized to generate power in power generationstage 360. Power generated by the power generation stage can be used forair separation 370, in which oxygen enriched air can be produced tosupply oxygen to the gasification stage. The cleaned syngas from thesyngas cleaning stage can then flow to a water-gas shift reaction stage350. This stage can produce a purified syngas stream for use as ahigh-value source of low-molecular weight gases, including hydrogen andcarbon oxides. The overall inputs into the gasification system includeorganic feed material and air, and the overall outputs include purifiedsyngas, ash, exhaust, and nitrogen. In some examples, the syngascleaning stage can produce usable fuel such as unreacted hydrocarbons orcarbon-char. These can be used to generate power for air separation.Additionally, these fuels can be used by the pulse detonation burners topower the gasifier and/or reformer.

FIG. 4 shows a schematic of a more specific example gasification system400. The system includes a gasifier 402, a reformer 404, a syngascleaning column 406, and a water-gas shift column 408. Similar to thegasifier shown in FIG. 1, the gasifier includes a gasifier body 410, afeeder 420, and a pulse detonation burner 430. A conical portion 412 ofthe gasifier body expands upward from the bottom of the gasifier body.The pulse detonation burner can be supplied with air or oxygen enrichedair through air line 432 and fuel through fuel line 434. The feeder canbe positioned to feed an organic material into the gasifier body.

Syngas and residual materials, such as organic vapors, tar, carbon-char,and mineral ashes, can flow out of the gasifier through an outlet 440.The reformer 404 can receive the syngas and residual materials from theoutlet 440 of the gasifier 402. The reformer includes a reformer body450 and a second pulse detonation burner 460 located above the reformerbody. The second pulse detonation burner can be connected to thereformer body to direct supersonic shockwaves downward into the reformerbody to heat the synthesis gas and residual material. The second pulsedetonation burner can also include a second air line 462 and a secondfuel line 464 to provide air or oxygen enriched air and fuel to thesecond pulse detonation burner. The reformer can operate similarly to aventuri ejector. The reformer body can include a venturi constriction470 to decrease pressure inside the reformer and draw the effluent fromthe gasifier into the reformer. The heat and mechanical energy providedby the second pulse detonation burner can convert unreacted residuals inthe gasifier effluent into additional syngas. The product gases from thereformer, including syngas and remaining residual materials, can flowout of the reformer through reformer outlet 480. In the example shown inFIG. 4, the reformer also has an ash outlet 490 where ash can be removedfrom the reformer.

The crude syngas produced by the reformer 404 can flow into the syngascleaning column 406. In the syngas cleaning column, any remainingcontaminants entrained in the syngas stream are separated from thesyngas product stream. The contaminants can be removed through acontaminant outlet 492 at the bottom of the syngas cleaning column.Following the reformer, two or more hot-cyclones operated in series maybe employed to remove carbon-char and mineral-ash. Due to the pulsingnature of the gas-flow, these cyclones can operate at high centrifugalvelocity, and thus high-efficiency, but without the normal highpressure-drop. Hot-cyclones typically need to operate at greater than100-ft/sec, which requires at least 0.2-psig pressure-drop. Thepressure-drop is not significant, but the constriction in the pipetypically required to generate 100-ft/sec can cause problems, e.g. byrestricting rapidly changing gas flow that is inherent to gasification.Pulse-detonations that power the Reformer solve this problem by drivingthe cyclone separators at high-velocity without the need forconstrictions in the gas clean-up piping. The syngas product then flowsto the water-gas shift column 408. The water-gas shift column can formadditional syngas from water vapor and carbon monoxide to produce thefinal purified syngas product stream 494.

The present technology also extends to methods of producing synthesisgas. FIG. 5 is a flowchart of one example method 500 of producingsynthesis gas. The method includes: introducing an organic material intoa gasifier comprising a gasifier body and a pulse detonation burnerlocated under the gasifier body 510; firing supersonic shockwaves fromthe pulse detonation burner upward into the gasifier body to heat theorganic material and form a jet spouted bed of the organic material 520;and removing synthesis gas and residual ash from the gasifier through anoutlet located at an upper portion of the gasifier body 530.

In various other examples, methods of producing synthesis gas caninclude any of the process equipment, operational parameters, processingstages, and other features described above, including an inverseoperation firing the first pulse detonation burner downward (e.g. as anentrained flow reactor) in an upside down embodiment with the reformingflowing upwards. The described features, structures, or characteristicsmay be combined in any suitable manner in one or more examples. In thepreceding description numerous specific details were provided, such asexamples of various configurations to provide a thorough understandingof examples of the described technology. One skilled in the relevant artwill recognize, however, that the technology may be practiced withoutone or more of the specific details, or with other methods, components,devices, etc., or firing in a horizontal direction. In other instances,well-known structures or operations are not shown or described in detailto avoid obscuring aspects of the technology.

The foregoing detailed description describes the invention withreference to specific exemplary embodiments. However, it will beappreciated that various modifications and changes can be made withoutdeparting from the scope of the present invention as set forth in theappended claims. The detailed description and accompanying drawings areto be regarded as merely illustrative, rather than as restrictive, andall such modifications or changes, if any, are intended to fall withinthe scope of the present invention as described and set forth herein.

What is claimed is:
 1. A pulsed detonation shockwave gasifiercomprising: a gasifier body; a feeder positioned to feed an organicmaterial into the gasifier body; a pulse detonation burner locatedeither: under the gasifier body and connected to the gasifier body todirect supersonic shockwaves upward into the gasifier body to heat theorganic material and to form a jet spouted bed of the organic materialor above the gasifier body and connected to the gasifier body to directsupersonic shockwaves downward into the gasifier body to heat theorganic material as an entrained flow reactor; and an outlet connectedto the gasifier body.
 2. The gasifier of claim 1, wherein the pulsedetonation burner produces shockwaves at a frequency of at least 2 Hz.3. The gasifier of claim 1, wherein the pulse detonation burner produceshot gas at a temperature from 750° C. to 3000° C.
 4. The gasifier ofclaim 1, wherein the pulse detonation burner is located under thegasifier body and the gasifier body comprises a conical portionexpanding upward from a lower portion of the gasifier body.
 5. Thegasifier of claim 1, further comprising a fuel source to supply ahydrocarbon fuel to the pulse detonation burner and an oxygen-enrichedair source to supply oxygen enriched air to the pulse detonation burner.6. A gasification system, comprising: a gasifier according to claim 1; areformer connected to the outlet of the gasifier to receive synthesisgas and residual ash from the gasifier, wherein the reformer comprises:a reformer body, a second pulse detonation burner located either aboveor below the reformer body and connected to the reformer body to directsupersonic shockwaves downward or upward into the reformer body to heatthe synthesis gas and residual ash.
 7. The gasification system of claim6, wherein at least one of the pulse detonation burner of the gasifierand the second pulse detonation burners produces shockwaves at afrequency of at least 2 Hz.
 8. The gasification system of claim 6,wherein at least one of the pulse detonation burner of the gasifier andthe second pulse detonation burners produces hot gas at a temperaturefrom 750° C. to 1550° C.
 9. The gasification system of claim 6, whereinthe reformer body comprises a venturi throat connected to the secondpulse detonation burner such that hot gas from the pulse detonationburner acts as a motive fluid to draw the synthesis gas and residual ashfrom the gasifier into the reformer.
 10. A method of producing synthesisgas, comprising: introducing an organic material into a gasifiercomprising a gasifier body and a pulse detonation burner connected tothe gasifier body; firing supersonic shockwaves from the pulsedetonation burner into the gasifier body to heat the organic materialusing a detonation fuel including a mixture of a hydrocarbon fuel withoxygen-enriched air; and removing synthesis gas and residual ash fromthe gasifier through an outlet located at an upper portion of thegasifier body.
 11. The method of claim 10, wherein the pulse detonationburner is located under the gasifier body and wherein the firing directsthe supersonic shockwaves upward into the gasifier body sufficient toform a jet spouted bed of the organic material.
 12. The method of claim10, wherein the firing directs the supersonic shockwaves downward orsideways into the gasifier body to operate as an entrained flow reactor.13. The method of claim 10, wherein the supersonic shockwaves are firedat a frequency of at least 2 Hz.
 14. The method of claim 10, wherein thesupersonic shockwaves travel at a velocity from 100 m/s to 3,000 m/s.15. The method of claim 10, wherein the pulse detonation burner produceshot gas at a temperature from 750° C. to 3000° C.
 16. The method ofclaim 10, wherein the oxygen-enriched air has 30 mole % to 99.9 mole %oxygen.
 17. The method of claim 16, wherein the fuel comprises at leastone of carbon-char residues recycled from the gasifier,micronized-carbon sourced from biochar, torrefied biomass, and coalfines, which is optionally entrained by a carrier fluid.
 18. The methodof claim 10, wherein the supersonic shockwaves comminute the organicmaterial to a smaller particle size than an initial particle size of theorganic material.
 19. The method of claim 18, wherein the initialparticle size of the organic material is from 1 mm to 10 cm.
 20. Themethod of claim 10, further comprising feeding effluent from thegasifier to a reformer, wherein the reformer comprising a reformer bodyand a second pulse detonation burner located above or below thereformer, wherein the second pulse detonation burner fires supersonicshockwaves downward or upward into the reformer body to heat theeffluent.
 21. The method of claim 20, wherein the reformer bodycomprises a venturi throat connected to the second pulse detonationburner such that hot gas from the pulse detonation burner acts as amotive fluid to draw the effluent into the reformer.
 22. The method ofclaim 10, wherein the synthesis gas comprises hydrogen and carbonmonoxide.